SYSTEM AND METHOD FOR PRODUCING LOW NOx AIR EMISSIONS FROM GASIFICATION POWER PLANTS

ABSTRACT

An apparatus is provided that receives waste and generates electrical power or thermal energy with minimal NOx emissions. A gasifier is provided that receives the waste and air to produce fuel gas for delivery to a fluidly coupled reformer. The reformer receives the fuel gas, recycled flue gas, and air to auto-thermally produce a reformed fuel gas and destroy fuel gas pollutants at a first temperature without a catalyst. A burner is fluidly coupled to the reformer and receives recycled flue gas and air to oxidize the reformed fuel gas at a second temperature that prevents nitrogen oxide formation, the second temperature being lower than the first temperature. A quench chamber is fluidly coupled to the burner and receives flue gas from the burner for quenching with recycled flue gas. A heat recovery system is fluidly coupled to the reformer, burner, and quench chamber to extract usable energy.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application claims priority to U.S. Provisional Application62/388,396, filed on Jan. 28, 2016, the complete disclosure of which isincorporated herein by reference in its entirety.

FIELD OF THE TECHNOLOGY

The present technology relates generally to gasification systems andmore particularly to multi-stage gasification systems that thermallyprocess carbonaceous solid waste to produce exportable energy and lowNOx air emissions and still more particularly to a multi-stage burnersystem that combusts fuel gas, produced by waste gasification, in a waythat minimizes fuel NOx, prompt NOx, and thermal NOx formation using aflue gas recycling system.

BACKGROUND OF THE TECHNOLOGY

A majority of municipal solid waste (“MSW”) is collected by trash trucksand transported to landfills where it is dumped into designated areas.When a dumping cell is full, it is sealed with a plastic sheet andcovered in several feet of dirt. The buried MSW causes severalenvironmental hazards as it decomposes, including generation ofgreenhouse gases (“GHG”) such as carbon dioxide (CO₂) and methane (CH₄).

MSW includes everyday items that are discarded by the public. Forexample, MSW may include biodegradable waste, inert waste, combustibleconstruction and demolition waste, composite waste, certain types ofhazardous or toxic waste, biomedical waste, and/or recyclable materials.The composition of MSW may vary greatly from municipality tomunicipality and may change over time. The MSW may originate fromresidential, commercial, institutional, and/or industrial sources.

Rather than burying the MSW in landfills, the MSW may be combusted toreduce the GHG equivalent levels below those produced through buryingthe MSW in landfills. Furthermore, the MSW may be combusted to recoverenergy from the waste. The conversion of waste-to-energy (“WTE”) may beperformed at a WTE facility. The MSW may be sorted and shredded toproduce refuse derived fuel (“RDF”) that is used to fire boilers thatproduce steam used to generate electrical power. For example, wasteincinerator systems are known to generate process steam and/orelectrical power while reducing MSW volume and mass. However,conventional incinerator systems often suffer from inadequate emissioncontrols that degrade the atmosphere with hazardous air pollutantsincluding acid gases, volatile organic compounds, and particulatematter, including heavy metals. For example, conventional incineratorsystems produce high levels of nitrogen oxides (NOx), as well as oxidesof sulfur (SO_(x)) hydrochloric acid, dioxins and furans, fineparticulate matter, and toxic metals, among other undesirablebyproducts.

With respect to NOx formation during combustion, the three primary NOxcontributors include (1) fuel NOx, (2) prompt NOx, and (3) thermal NOx.Fuel NOx is formed during combustion when a partially decomposingcomponent specie having a carbon-nitrogen bond is oxidized, either byoxygen or a hydroxyl species. Prompt NOx follows a similar pathway tofuel NOx with a distinction that prompt NOx is typically associated withhigh energy density fuels such as natural gas, with free radicalformation occurring within the fuel rich region of the combustion zoneflame. Thermal NOx is formed at very high temperatures associated withthe high energy requirement to break a nitrogen-nitrogen triple bond andenable oxidation to a NOx specie. While the reaction rates for each ofthese three NOx formations are different, all NOx is formed as afunction of oxygen concentration and temperature. Furthermore,conventional incinerator systems produce solid residues that requirespecial storage arrangements to prevent un-combusted organics and heavymetal contaminants from leaching into ground water. These and otherdrawbacks exist with conventional incinerator technology.

BRIEF DESCRIPTION OF THE FIGURES

FIG. 1 illustrates a multi-stage gasification system according to oneexample of the technology;

FIG. 2 illustrates a multi-stage gasification system for convertingsolid waste and/or biomass into power by waste gasification in a shallowfluid bed and a residue kiln gasifier with staged reforming andcombustion of the fuel gas produced with low levels of NO_(x) gaseousemissions;

FIG. 3 illustrates an isometric view of a multi-stage gasificationsystem including an updraft gasifier for a primary thermal reactor and arotary kiln as a secondary thermal reactor according to one example ofthe technology;

FIG. 4 illustrates a cross-sectional view of a reformer-burner-quenchunit for reforming, combusting, and quenching the fuel gas produced bythe gasifiers according to one example of the technology;

FIG. 5 illustrates a flowchart of an example method according to oneexample of the disclosure; and

FIG. 6 illustrates a flowchart of an example method according to anotherexample of the disclosure.

DETAILED DESCRIPTION OF THE TECHNOLOGY

It will be appreciated that for simplicity and clarity of illustration,where appropriate, reference numerals may be repeated among thedifferent figures to indicate corresponding or analogous elements. Inaddition, numerous specific details are set forth in order to provide athorough understanding of the examples described herein. However, itwill be understood by those of ordinary skill in the art that theexamples described herein can be practiced without these specificdetails. In other instances, methods, procedures, and components havenot been described in detail so as not to obscure the related relevantfeature being described. Also, the description is not to be consideredas limiting the scope of the examples described herein. The drawings arenot necessarily to scale and the proportions of certain parts may havebeen exaggerated to better illustrate details and features of thepresent disclosure. Those skilled in the art with access to theteachings provided herein will recognize additional modifications,applications, and examples within the scope thereof and additionalfields in which the technology would be of significant utility.

Unless defined otherwise, technical and scientific terms used hereinhave the same meaning as is commonly understood by one of ordinary skillin the art to which this disclosure belongs. The terms “first,”“second,” and the like, as used herein do not denote any order,quantity, or importance, but rather are used to distinguish one elementfrom another. Also, the terms “a” and “an” do not denote a limitation ofquantity, but rather denote the presence of at least one of thereferenced items. The term “or” is meant to be inclusive and meanseither, any, several, or all of the listed items. The terms“comprising,” “including” and “having” are used interchangeably in thisdisclosure. The terms “comprising,” “including” and “having” mean toinclude, but are not necessarily limited to the things so described.

The terms “connected” and “coupled” are not restricted to physical ormechanical connections or couplings, and can include electricalconnections or couplings, whether direct or indirect. The connection canbe such that the objects are permanently connected or releasablyconnected. The term “communicatively coupled” is defined as connected,either directly or indirectly through intervening components, and theconnections are not necessarily limited to physical connections, but areconnections that accommodate the transfer of data, signals, or othermatter between the so-described components. The term “substantially” isdefined to be essentially conforming to the thing that it“substantially” modifies, such that the thing need not be exact. Forexample, substantially real-time means that the occurrence may happenwithout noticeable delay, but may include a slight delay.

The terms “circuit,” “circuitry,” and “controller” may include either asingle component or a plurality of components, which are either activeand/or passive components and may be optionally connected or otherwisecoupled together to provide the described function. The “processor”described in any of the various embodiments includes an electroniccircuit that can make determinations based upon inputs and isinterchangeable with the term “controller.” The processor can include amicroprocessor, a microcontroller, and a central processing unit, amongothers, of a general purpose computer, special purpose computer, ASIC,or other programmable data processing apparatus. While a singleprocessor can be used, the present disclosure can be implemented over aplurality of processors.

The “server” described in any of the various examples includes hardwareand/or software that provides processing, database, and communicationfacilities. By way of example, and not limitation, “server” may refer toa single, physical processor with associated communications and datastorage and database facilities, or it can refer to a networked orclustered complex of processors and associated network and storagedevices, as well as operating software and one or more database systemsand applications software that support the services provided by theserver.

For the purposes of this disclosure a computer readable medium storescomputer data in machine readable form. By way of example, and notlimitation, the computer readable medium may include computer storagemedia and communication media. Computer storage media includes volatileand non-volatile, removable and non-removable media implemented in anymethod or technology for storage of information such ascomputer-readable instructions, data structures, program modules orother data. Computer storage media includes, but is not limited to, RAM,ROM, EPROM, EEPROM, flash memory or other solid state memory technology,CD-ROM, DVD, or other optical storage, magnetic cassettes, magnetictape, magnetic disk storage or other magnetic storage devices, or anyother medium that may be used to store the desired information and whichcan be accessed by the computer.

The below description references block diagrams and operationalillustrations of systems and methods of gasifying municipal solid waste(“MSW”) or refuse derived fuel (“RDF”) to reduce volume and mass of MSW,while reducing greenhouse gases (“GHG”) and other pollutants belowlevels produced by conventional waste incinerator systems. Gasificationinvolves thermal processing of carbonaceous containing materials ormixtures of materials in an environment having insufficient oxygen tocompletely combust all of the feed materials and/or all of theby-products produced. A gasification reactor may include a device thatindirectly provides heat needed for gasification. A predominant productthat exits a gasification reactor is known as water gas, which includeswater, hydrogen, carbon dioxide, and carbon monoxide. Other productsthat exit a gasification reactor include light hydrocarbon gases,un-reacted atmospheric nitrogen and trace contaminants. Producer gasincludes a low calorific value due to its nitrogen content and is oftenimproperly referred to as synthesis gas or syngas.

The product that exits an air fed gasification device will be referredto throughout this disclosure as “fuel gas.” Fuel gas may containhydrocarbons; sulfur containing gases such as hydrogen sulfide and othergases; nitrogen containing gaseous species such as ammonia and othergases; halide containing gaseous species such as hydrochloric acid andother gases; and particulates. The particulates are commonly known asfly-ash when exiting the gasifier with gaseous products and bottom ashwhen exiting the gasifier in a solid or molten stream. If the gasifieris air fed, as opposed to oxygen blown, then a major component of thefuel gas that exits the gasifier will include di-molecular nitrogen. Thecombustible gas that exits a gasifier will be referred to as fuel gasthroughout this disclosure.

It is understood that each block of the block diagrams or operationalillustrations, and combinations of blocks in the block diagrams oroperational illustrations, can be implemented with analog or digitalhardware and computer program instructions. The computer programinstructions may be provided to a processor that executes the computerprogram instructions to implement the functions/acts specified in theblock diagrams or operational block or blocks. In some alternativeimplementations, the functions/acts noted in the blocks may occur out ofthe order noted in the operational illustrations. For example, twoblocks shown in succession may in fact be executed substantiallyconcurrently or the blocks may sometimes be executed in the reverseorder, depending upon the functionality/acts involved.

According to one example, the technology described herein includes amulti-stage gasification system that allows independent control ofgasification reactions in each of the two gasification reactors of themulti-stage gasification system. For example, gasification reactionsthat occur in a first gasifier may be controlled separately fromgasification reactions that occur in a second gasifier. According to oneexample, a processor having instructions stored thereon may regulatefluid flow throughout the multi-stage gasification system. According toone example, the processor may be programmed to operate the first andsecond gasifiers in an oxygen starved or sub-stoichiometric airenvironment. For example, the processor may be programmed to controldampers that feed oxygen to the first and second gasifiers. Suchoperation results in the production of a fuel gas, comprised mainly ofcarbon monoxide, hydrogen, and some methane and other light hydrocarbongases as combustible components and carbon dioxide, water vapor, andmolecular nitrogen as the main non-combustible components. After removalof particulates in high temperature cyclones, this fuel gas is directedto the reformer, burner, and quench units, which provide for stagedcombustion of the fuel gas. These burner and quench units, in aggregate,are operated with sufficient excess air to complete combustion andminimize pollution.

According to one example, control of the temperature and oxygen partialpressure in the first gasifier and the reformer, and the burner units isaccomplished, in part, with the controlled inlet of recycled flue gas.For example, the processor may open, close, or partially open/close avalve within a duct to control a flow of the recycled flue gas to thereformer and burner. According to one example, the processor may monitorthe temperature of gases within the first gasifier, the reformer, or theburner and may control valves that supply oxygen and/or recycled fluegas to these components. For example, if the processor measures atemperature within the reformer to be higher than a pre-selectedtemperature, then the processor may open a valve within a duct toincrease a flow of the recycled flue gas to the reformer and/or burner.Alternatively, the processor may open a valve to increase a flow ofoxygen into the reformer. According to another example, if the processormeasures a temperature within the reformer to be lower than apre-selected temperature, then the processor may close or partiallyclose a valve within a duct to reduce a flow of the recycled flue gas tothe reformer and/or burner. Alternatively, the processor may close avalve to decrease a flow of oxygen into the reformer. Furthermore, ifthe processor determines that a temperature within a portion of acomponent such as the reformer is too high or too low, then theprocessor may adjust valves to direct gas to or divert gas from selectedportions of a component.

According to another example, the multi-stage gasification system allowsindependent control of parameters at various points throughout themulti-stage gasification system. The parameters may be controlled toreduce or avoid formation of hazardous pollutants. According to oneexample, the parameters may include gas temperature, gas residence time,pressure, flow rate, and oxygen content. According to one example, theparameters may be controlled to adjust for changes in the composition ofMSW fed into the multi-stage gasification system. According to oneexample, the parameters may be controlled to adjust for changes in thecomposition of MSW fed into a single-stage gasification system.

According to yet another example, the technology may employ asingle-stage gasification system instead of a multi-stage gasificationsystem. According to one example, a gasifier in a single-stagegasification system may be operated at a higher temperature with shorterreaction times compared to gasifier in a multi-stage gasificationsystem. According to one example, a rotating kiln may be employed in asingle-stage gasification system, without the need for a secondgasification stage. According to this example, the rotating kiln mayoperate at a sufficiently high temperature, with sufficient reactiontime, to ensure complete gasification of the waste. For example, MSW maybe fed to a rotating kiln, which may produce an inert ash and a fuelgas. According to one example, the fuel gas may be utilized in a samemanner as the fuel gas produced by a multi-stage system.

FIG. 1 illustrates a multi-stage gasification system 100 according toone example of the technology that includes a primary gasifier 102, asecondary gasifier 106, a reformer 109, a burner 113, a quench chamber117, a boiler 120, and an air pollution control system 126. According toone example, fuel 130 such as refuse derived fuel (“RDF”) may bedeposited into the primary gasifier 102 via a duct 101. The fuel 130 mayinclude MSW, shredded waste, source separated waste, construction anddemolition debris, light combustibles, medical waste and/or biomass, orthe like. According to one example, the fuel 130 may be made up ofmaterials that contain carbon, hydrogen, oxygen, nitrogen, sulfur,chlorine, as well as other elements found in the various forms of solidwaste. For example, the fuel 130 also may include elements such asphosphorus, silicon and aluminum. The fuel 130 may be blended with anauxiliary fuel or a higher energy content fuel such as tire shreds, oil,or the like, to promote combustion. According to one example, the fuel130 may be stored in a feeding bin such as an automated feeding bin orthe like. According to one example, the fuel 130 may be transported intothe primary gasifier 102 via a feeder such as a conveyor belt, corkscrew, gravity chute, or the like. According to one example, the feedermay fluidly couple the primary gasifier 102 and the secondary gasifier106.

According to one example illustrated in FIG. 1, the multi-stagegasification system 100 gasifies the fuel 130 in two stages. One ofordinary skill in the art will readily appreciate that the multi-stagegasification system 100 may employ more than two stages. According toanother example, a single-stage gasification system may be used.According to one example, the feeder may transport char and ash from theprimary gasifier 102 into the secondary gasifier 106 through a duct 105.The char and ash may include a non-sintered carbonaceous solidcontaining residue for conversion in the secondary gasifier 106 to acarbonless, sintered ash. According to one example, the secondarygasifier 106 may be configured to receive the fuel 130 directly thereinto supplement the char and ash received therein.

According to one example, sub-stoichiometric quantities of air receivedfrom air sources 132, 134 may be fed into the primary gasifier 102 andthe secondary gasifier 106 via ducts 103, 107, respectively. Accordingto one example, the two stage gasification configuration permitsindependent control of temperature and gas composition in each of theprimary gasifier 102 and the secondary gasifier 106. Independent controlof gasifier parameters may allow a reduction in pollutant formation.Alternatively, the independent control of gasifier parameters mayeliminate formation of pollutants. According to one example, the twostage gasification configuration may provide complete carbon conversion,which may result in an inert ash product. In other words, the secondarygasifier 106 may complete combustion of unreacted carbon in ash productreceived from the primary gasifier 102.

With respect to temperature ranges during operation, the primarygasifier 102 may operate in a range of 1000° F. to 1800° F., forexample. According to one example, the primary gasifier 102 may operateat a preferred temperature of 1400° F. According to one example, thesecondary gasifier 106 may operate in a range of 1900° F. to 2100° F.,for example. According to one example, the secondary gasifier 106 mayoperate at a preferred temperature of 2000° F. One of ordinary skill inthe art will readily appreciate that the operating temperature of thesecondary gasifier 106 will depend on the melting point of the ashportion of the fuel and whether consolidation (sintering) or slagging isdesired. One of ordinary skill in the art will further readilyappreciate that the operating temperature of the primary gasifier 102and the secondary gasifier 106 may fall outside these ranges.

According to one example, the primary gasifier 102 may be a fluid bedgasifier wherein the fuel 130 and/or biomass is placed in an inert bedof fluidized material such as char, sand, or the like. According to oneexample, the primary gasifier 102 is a rotating kiln. According to oneexample, the fuel 130 and/or biomass may be fed either above-bed ordirectly into the bed, depending on a size and density of the fuel 130and/or biomass. During operation, the bed material may be maintained ata preselected temperature. According to one example, drying, pyrolysis,oxidation, and reduction reactions may occur simultaneously. Accordingto one example, the temperature at the top of the gasifier may be 100°F.-150° F. lower than the temperature at the bottom of the gasifier.

According to one example, the multi-stage gasification system 100 mayinclude a reformer 109 that is fluidly coupled to the primary gasifier102 via a duct 104 and is fluidly coupled to the secondary gasifier 106via a duct 108. According to one example, the reformer 109 receivesprimary fuel gas that is generated in the primary gasifier 102 throughduct 104 and secondary fuel gas that is generated in the secondarygasifier 106 through duct 108. According to one example, the reformer109 may be fluidly coupled to an air source 134 through duct 110 and maybe fluidly coupled to recycled flue gas exiting the heat recovery system120, typically a boiler or flue gas heat exchanger, via duct 111.According to one example, the reformer 109 may receive air from airsource 134 through duct 110 and a portion of the recycled flue gas fromthe boiler 120 through duct 111. According to one example, the reformer109 thermally cracks and reforms volatilized hydrocarbons that aregenerated in the primary gasifier 102 and the secondary gasifier 106 toform predominantly water gas species. According to one example, thewater gas species may include hydrogen, water, carbon monoxide, andcarbon dioxide, along with minor quantities of light hydrocarbon gasesand readily combustible soot carbon particles.

According to one example, the reformer 109 may provide a reducing gasatmosphere that substantially thermally decomposes any ammonia that waspredominantly formed in the primary gasifier 102. According to oneexample, the reformer 109 may substantially thermally decompose theammonia into nitrogen and hydrogen. For example, the processor mayregulate and control the composition and flow rate of gases through themulti-stage gasification system 100 in order to maintain a temperaturewithin the reformer 109 in a range that thermally decomposes the ammoniainto nitrogen and hydrogen. According to one example, the reformer 109may convert the ammonia produced from organic nitrogen provided in thefuel 130 to minimize production of fuel NOx. Accordingly, themulti-stage gasification system 100 substantially eliminates a precursorto fuel NOx formation. According to one example, any inert gases such asnitrogen and argon provided within the reformer 109 may remain virtuallyun-reacted.

According to one example, the multi-stage gasification system 100 mayinclude a processor with instructions stored thereon that regulate fluidflow throughout the multi-stage gasification system 100. According toone example, the processor may be electrically coupled to one or moregas regulators that control opening and closing of internal dampers orvalves in order to direct fluid flow through ducts within themulti-stage gasification system 100. For example, the processor may beprogrammed to set the internal valves within the ducts to fully open,fully closed, partially open, or partially closed. The gas regulatorsmay be fluidly coupled to gas sources that provide gases to themulti-stage gasification system 100 such as air, oxygen, carbon dioxide,carbon monoxide, nitrogen, and hydrogen, among other gases. Themulti-stage gasification system 100 may further include sensors that areelectrically coupled to the processor. The sensors may be configured tomeasure values such as temperature, fluid flow, gas concentration, andenergy content, among other values. According to one example, theprocessor may electrically communicate with gas regulators, gas sources,blowers, and sensors, among other devices, to establish and maintaindesired operating conditions within the multi-stage gasification system100. For example, the processor may control dampers located within theducts to determine a quantity of flue gas that is recirculated to thevarious components of the multi-stage gasification system 100.

Furthermore, the processor may control one or more gas regulators tometer a quantity of gas such as oxygen that is provided through theducts to the various components of the multi-stage gasification system100. The processor also may control a motor that drives a feedersupplying the fuel 130 into the first and/or second gasifiers 102, 106.For example, the processor may control the speed of feeder. According toone example, the multi-stage gasification system 100 may include aplurality of feeders that separately feed fuel 130 components such asthe MSW, the shredded waste, the source separated waste, theconstruction and demolition debris, the light combustibles, and/or thebiomass, or the like, into the first and/or second gasifiers 102, 106.The processor may control one or more motors that drive multiple feedersto provide a desired blend of fuel 130.

According to one example, the processor may regulate oxygen flow rateswithin the multi-stage gasification system 100 to maintain the oxygenpartial pressure in the reformer 109 at sub-stoichiometric levels. Forexample, the amount of oxygen fed into the reformer 109 may result inoxygen utilization of only 90-95% compared to an amount needed forcomplete combustion. According to one example, an optimal ratio of fuelgas, air, and recycled flue gas within the reformer 109 will depend onmultiple factors including the composition of the fuel gases receivedfrom the primary and secondary gasifiers 102, 106; a fluid flow ratewithin the ducts 104, 108; an amount of excess oxygen received in therecycled flue gas through duct 111; and the temperatures of each stream,among other factors. According to one example, a temperature of thegases provided to the reformer 109 is greatly increased. With respect toa temperature range during operation, the reformer 109 may operate in arange of 1900° F. to 2500° F. or higher, for example. One of ordinaryskill in the art will readily appreciate that the operating temperatureof the reformer 109 may fall outside these ranges. According to oneexample, the operating temperature may be controlled by a ratio ofambient air provided via air source 134 and recycled flue gas providedvia duct 111.

According to one example, the content of the fuel 130 and/or the biomassmay change over time since waste composition varies over time. Forexample, the presence of paper products in the MSW may increase chlorinecontent, while the presence of carpet in the MSW may increase nitrogencontent. According to one example, the processor may monitor sensorsthroughout the multi-stage gasification system 100 and may adjust systemcomponents such as dampers located within the ducts to maintain desiredsystem parameters such as temperature, fluid flow, and gasconcentrations, or the like, in order to maintain equilibriumconditions. For example, dampers may be adjusted to adjust a flow ofrecycled flue gas into the various system components to controloperating temperatures. In this way, the processor is capable ofadjusting the multi-stage gasification system 100 to process fuel 130and/or the biomass having any of a variety of compositions, includingthose typical of light construction and demolition waste, sourceseparated commercial waste, residential municipal solid waste andagricultural biomass. The processor will control each stage'stemperature and find the temperatures and recycled flue gas flow to eachbranch to minimize the NOx formed for each fuel type.

According to one example, the reformer 109 is maintained at a hightemperature to facilitate decomposition of ammonia in the fuel gas.According to one example, the reformer 109 may operate in a range of1900° F. to 2500° F., for example. According to one example, the hightemperature provided in the reformer 109 increases the decompositionrate of ammonia into diatomic nitrogen and hydrogen by making theammonia less thermodynamically favorable. Furthermore, the hightemperature provided in the reformer 109 facilitates a steam reformingreaction in which water vapor reacts with hydrocarbons in the fuel gasto produce hydrogen and carbon monoxide. According to one example, thereformer 109 may be sized to provide a predetermined amount of residencetime for the fuel gas to be reformed. According to one example, thereformer 109 may be sized to provide at least two seconds of residencetime for the fuel gas to be reformed. One of ordinary skill in the artwill readily appreciate that the amount of residence time may varydepending on the temperature maintained in the reformer 109 and the gasflow rate.

According to one example, the reformer 109 does not utilize a catalyst.This provides the multi-stage gasification system 100 with advantagesover conventional gasification systems that utilize a catalyst. Forexample, operating the reformer 109 without a catalyst reduces thepressure drop across the reformer 109 and reduces operational costs.

Advantages of the multi-stage gasification system 100 over conventionalgasification systems may be demonstrated through computation of theequilibrium composition of the gases as a function of the gastemperature in the reformer 109. An assumption may be made that all ofthe organic nitrogen in the fuel is converted to ammonia in the reducingatmosphere of the primary gasifier 102. According to one example, theprimary gasifier 102 may be operated at a temperature betweenapproximately 1,200° F. and 1700° F. At these temperatures, thermaldecomposition is relatively small for the typical range of nitrogen,hydrogen, and ammonia compositions produced by gasification of wastetypes described herein.

With respect to computing reaction equilibrium, data for publishedequilibrium constant Kp by Brown et. al. may be used for the Haberprocess in which ammonia is formed by the reaction of nitrogen andhydrogen. The extent to which the reverse reaction occurs may beestimated.

A chemical equation for the formation of ammonia from its elements is:

N₂±3H₂→2NH₃

An equilibrium concentration of ammonia in the reformed fuel gas may beestimated using the following equation:

C _(NH3)=√{square root over (K _(P)(RT)^(Δn) C _(N2) C _(H2) ³)}

where C_(NH3), C_(N2), and C_(H2) are molar concentrations of ammonia,nitrogen, and hydrogen gases in moles per liter. The ammonia molarconcentration is typically small compared to the nitrogen and hydrogenmolar concentrations. According to one example, any ammonia remaining inthe exhaust gases of the reformer 109 may be estimated from the air andthe recycle gas utilization, the hydrogen from the carbon, hydrogen, andoxygen atom balances, and the water gas shift equilibrium, assuming theresidual hydrocarbon gases are negligible compared to the water gasspecies.

Alternatively, an approximation of an improved performance of themulti-stage gasification system 100, as compared to conventionalgasification systems, may be made by comparing results of operating thereformer 109 at a higher temperature than the primary gasifier 102.According to one example, the approximation is determined by computing apercent reduction in ammonia concentration from a base case of a valueat 700° C. (1,292° F.), which is effectively proportional to the squareroot of the ratio of the equilibrium constants at 700° C. divided by thevalue at the higher temperature. The results are presented in Table 1below.

TABLE 1 Estimation of The % Reduction in NOx Relative to 700° C. T ° C.KP % Reduction in NOx Relative to 700° C. 700 5.096 × 10⁻⁰⁷ 00.0% 8001.522 × 10⁻⁰⁷ 45.3% 900 5.586 × 10⁻⁰⁸ 66.9% 1000 2.400 × 10⁻⁰⁸ 78.3%1100 1.166 × 10⁻⁰⁸ 84.9% 1200 6.249 × 10⁻⁰⁹ 88.9% 1300 3.625 × 10⁻⁰⁹91.6%

According to one example, a majority of the chemical energy or higherheating value is converted to sensible heat and partial combustionproducts in the reformer 109 in order to mitigate against having a highenergy density localized fuel gas to burn in the burner 113. Thesensible heat corresponds to changes in temperature of the gas without achange in phase. In this way, the reformer 109 operates to minimizeprompt NOx formation. According to one example, adverse consequencessuch as formation of thermal NOx that may result from introducing higherthan normal higher fuel gas feed temperature into the burner 113 may bemitigated by burning and cooling the low energy content reformed fuelgas with a blend of warm recycle fuel gas and ambient air. Accordingly,the reformer 109 may be configured to limit total NOx formation in themulti-stage gasification system 100.

According to one example, the reformer product fuel gas that isgenerated in the reformer 109 may be delivered into the fuel gas burner113 through a duct 112. The fuel gas burner 113 also may receive airfrom an air source 136 through a duct 114 and may further receive aportion of the recycled flue gas that originates from the boiler 120through a duct 115. According to one example, the fuel gas burner 113may be dimensioned to provide the reformer product fuel gas withsufficient gas residence time at a sufficient temperature to completelycombust all carbonaceous and hydro-carbonaceous materials.

According to one example, the fuel gas burner 113 may be controlled tolimit the oxygen content and the temperature therein so as to minimizeNOx formation. For example, the fuel gas burner 113 may be controlled toadjust the temperature to approximately under 1800° F. by adjusting theratio of ambient air and recycled flue gas. According to one example,the temperature in the fuel gas burner 113 may be selected to limitthermal NOx formation to insignificant levels, while providingsufficient heat in the fuel gas burner 113 to quickly destroy dioxins,furans, and any remaining carbonaceous and hydro-carbonaceous material.One of ordinary skill in the art will readily appreciate that an optimalratio of reformed fuel gas from the reformer 109, air from the airsource 136, and the recycled flue gas originating from the boiler 120will depend on multiple factors including a composition of the reformedfuel gas, an amount of excess oxygen in the recycled flue gas, and thetemperature of each stream, among other factors. One of ordinary skillin the art will readily appreciate that the fuel gas burner 113 may bemaintained at any desired temperature, below the adiabatic flametemperature of the fuel gas. According to one example, the fuel gasburner 113 may control combustion of the reformed fuel gases to minimizeproduction of thermal NOx.

According to one example, the burner product flue gas that originatesfrom the fuel gas burner 113 may be introduced into the quench chamber117 through a duct 116. The quench chamber 117 also may receive aportion of the recycled flue gas that originates from the boiler 120through a duct 118. According to one example, the quench chamber 117 maybe dimensioned to provide the burner product fuel gas with sufficientgas residence time to cool by mixing with the portion of the recycledflue gas received through the duct 118. According to one example, theburner product flue gas may be cooled prior to delivery into a heatrecovery system 120 in order to solidify any molten mineral matterentrained in the resulting quench flue gas. The quench flue gas, withany molten mineral matter solidified, may be transported to the heatrecovery system 120 via a duct 119. According to one example, the moltenmineral matter may be solidified to avoid fouling the heat recoverysystem tubes or other parts such as by having mineral matter stickthereto. The quench chamber 117 is further configured to avoid acid gasattack on the heat recovery system tubes. In this way, the quenchchamber 117 is designed to maintain clean system parts in order toextend the useful life of the system, including the heat recovery system120.

According to one example, a target cooling temperature for the quenchflue gas may be determined by heat recovery system specifications. Forexample, the quench flue gas may be cooled to approximately 1400° F.based on heat recovery system specifications. One of ordinary skill inthe art will readily appreciate that other target cooling temperaturesmay be selected based on boiler specifications. There are advantages toquenching the burner product flue gas with the recycled flue gas ratherthan quenching with air. For example, the recycled flue gas maintains anoverall excess oxygen at a desired level in the flue gas stream.According to one example, controlling excess oxygen in the exhaust mayimprove performance of the air pollution control system 126 by reducingthe dilution of pollutants. Furthermore, using recycled flue gas allowsa reduction in total volume of flue gas that passes through a downstreamair pollution control system 126. According to one example, using therecycled flue gas reduces a flow rate through the air pollution controlsystem 126, which allows for reductions in equipment size, heat loss,and capital costs. Additionally, recycled flue gas includes a highermoisture content as compared to ambient air. According to one example, ahigher moisture content allows for more efficient operation of theelectrostatic precipitator of the air pollution control system 126.Still further, using recycled flue gas provides better overall plantefficiency by lessening a flow of hot gas out of the stack.

According to one example, suitably treated boiler feed water 138 may bepumped into the heat recovery boiler 120 via pipe 121. According to oneexample, the heat recovery system 120 may include a heat energy recoverysystem such as a heat exchanger that transfers a portion of sensibleheat from the quench flue gas 119 to the boiler feed water 138. The heatrecovery system 120 generates product steam 140 that is delivered to agenerator via pipe 122 in order to produce electrical power.Alternatively, the heat recovery system 120 may include a heatrecirculating thermal oil that drives an organic Rankine cycle systemthat generates electrical power. In an organic Rankine cycle, instead ofusing steam as the working fluid, a refrigerant is used in a closed loopin which the refrigerant is heated by a heat transfer fluid thatextracts the sensible heat from the hot flue gases. The refrigerantexpands as it is heated and drives a turbine whose shaft rotates andproduces power in a generator. According to one example, the heatrecovery system 120 may operate with an exhaust in a range of 600° F. to800° F., for example. According to one example, the heat recovery system120 may operate at a preferred exhaust temperature of 700° F. whenoptimizing subsequent SCR treatment for NOx emissions reduction.

According to one example, a high proportion of the heat recovery systemexhaust flue gas may be diverted from the heat recovery system 120 via aduct 123 and may be distributed as recycled flue gas through ducts 111,115, 118, 124, and 125. While a conventional system may recycle 20-40%of the heat recovery system flue gas, the multi-stage gasificationsystem 100 described herein may recycle 60-75% of the heat recoverysystem's exhaust flue gas. An optimal percentage of heat recovery systemrecycled flue gas will depend on a desired amount of excess oxygencontained in the boiler flue gas. According to one example, less recycleboiler flue gas is needed with a higher concentration of excess oxygenin the flue gas. According to one example, any boiler flue gas that isnot recirculated to the quench chamber 117, the burner 113, and/or thereformer 109 may be diverted to the air pollution control system 126 viaduct 125 for cleaning. According to one example, the cleaned heatrecovery system's exhaust flue gas may be vented to the atmosphere via astack 127.

Air pollution control systems are typically employed for post formationcontrol of most combustion products from MSW combustion systems such asNOx emissions, particulates, acids, heavy metals, volatile organiccompounds, or the like. For example, electrostatic precipitators as wellas fabric filters/bag-houses may be effective for removing particulates.Dry scrubbing is commonly used to remove sulfur oxides and hydrogenhalides. Injection of activated carbon upstream of the particulatecollection devices is effective for removal of heavy metals and volatileorganic compounds. Selective catalytic reduction (SCR) units aretypically employed to meet emissions standards. However, these devicesare expensive and provide a large footprint for MSW combustion systems.

According to one example, the multi-stage gasification system 100 isoperated to maintain equilibrium conditions such that any pollutants areemitted at or below air emissions standards for MSW combustion systems.Accordingly, the air pollution control system 126 of the presenttechnology may require few post formation control devices. However,given the dynamic and ever changing composition of the MSW that isprocessed by the multi-stage gasification system 100, the air pollutioncontrol system 126 may include devices that ensure compliance with airemissions standards such as a selective catalytic reduction (SCR) unit,an electrostatic precipitator (ESP), an acid-gas removal unit, a baghouse or other flue gas clean-up units. Depending on the air qualitystandards of an area, the NOx concentration within the boiler flue gasmay be sufficiently low as to not require catalytic reduction of theNOx. Avoiding use of post formation control devices such as catalyticreduction will save significant construction cost for the air pollutioncontrol system 126.

FIG. 4 illustrates a portion of the multi-stage gasification system 100including the fuel gas reformer 109, the fuel gas burner 113, and theflue gas quench chamber 117 according to one example of the technology.According to one example, the fuel gas reformer 109 may be a verticallyoriented cylindrical tube having multiple gasifiers that are fluidlycoupled thereto. According to one example, fuel gas from the multiplegasifiers may enter the reformer 109 through ducts 438 provided near thetop of the reformer 109. This reformer configuration may be advantageouswhen used with updraft gasifiers having high fuel gas outlets. Accordingto one example, annular headers 401 may be provided near the top of thereformer 109 to mix the fuel gas with a mixture air and the recycledflue gas during entry into the vertically oriented cylindrical tube.According to one example, the air and the recycled flue gas mixture maybe supplied to the reformer 109 through ducts 411. The top of thereformer 109 may include a short vent stack 403 that serves as anemergency bypass. According to one example, the short vent stack 403 mayvent any lighter-than-air fuel gas that may accumulate in the reformer109 during shut down.

According to one example, the reformer 109 may include annular headers401 with outlets that are offset from a central axis of the verticallyoriented cylindrical tube. According to one example, the outlets may bepositioned to promote a cyclonic gas flow through the reformer 109 inorder to promote mixing of the gases. According to one example, theoutlets may be oriented to reduce local temperature differences andpromote a complete reaction, which are important to minimize formationof prompt NOx. According to one example, the multi-stage gasificationsystem 100 may include fans, ducts, pipes, dampers, and/or baffles tofluidly couple the quench chamber 117, the burner 113, and the reformer109, along with other components.

According to one example, the reformer fuel gas is directed from thereformer 109 into the fuel gas burner 113 through a duct. According toone example, the burner 113 may include a rectangular-shaped duct.Alternatively, the burner 113 may include a cylindrical-shaped duct. Oneof ordinary skill in the art will readily appreciate that other ductshapes may be employed. According to one example, a duct 415 may beprovided in fluid communication with a plenum 402 in order to equallydistribute a mixture of air and recycled flue gas in the burner 113.According to one example, the plenum 402 may be shaped to evenlydistribute the mixture of air and recycled flue gas through a series ofnozzles 417. For example, the plenum 402 may be formed in a U-shape.According to one example, the nozzles 417 may be oriented to promoteeven mixing of the reformer fuel gas with the air and recycled flue gasmixture.

According to one example, the quench chamber 117 may be positioned afterthe burner 113. According to one example, the quench chamber 117 may bedimensioned to allow a predetermined residence time in order to destroyany tars remaining in the burner fuel gas. According to one example, aconfiguration of the quench chamber 117 may be similar to theconfiguration of the burner 113. According to one example, a duct 418may be provided at the quench chamber 117 to receive recycled flue gas.For example, the duct 418 may be provided at a top portion of the quenchchamber 117 to receive recycled flue gas.

FIG. 2 illustrates a multi-stage gasification system 200 according toone example of the technology that includes a primary gasifier 102, asecondary gasifier 106, a reformer 109, a burner 113, a quench chamber117, a boiler 120, and an air pollution control system 126, among othercomponents. According to one example, the multi-stage gasificationsystem 200 is a waste-to-energy conversion system that efficientlyconverts solid waste and/or biomass into steam that is used to generatepower. According to one example, the multi-stage gasification system 200is designed to minimize NOx emissions through staged fuel gas combustionand flue gas recycle. According to one example, refuse derived fuel(“RDF”) may be prepared from MSW, source separated waste, and/orconstruction and demolition debris light combustibles, or the like. TheRDF may be deposited into a fuel processing building 229 via a duct orchute 228. According to one example, the RDF may be blended with anauxiliary or higher energy content fuel such as tire shreds (“TDF”) orthe like. The TDF may be deposited into a fuel processing building 229via a duct or chute 230. The resulting fuel mixture is typically storedin an automated feeding bin that is contained within the facility fuelprocessing building 229.

According to one example, any water that is expelled from the fuelprocessing building 229 may be collected and routed through a pipe 231to a water treatment plant 288 for purification, re-use, and/ordisposal. For example, any water expelled during handling and shreddingof the waste, as well as any waste water generated from the building bypersonnel sanitary functions, may be collected and routed through thepipe 231 to the water treatment plant 288 for purification, re-use,and/or disposal. According to one example, any water needed at that thefuel processing building 229, including for sanitary functions, may beprovided through a pipe 233 from the water treatment plant 288.

According to one example, a fuel mix obtained through a duct 201 fromthe fuel processing building 229 may be transported into the primarygasifier 102 by a feeder such as an augured conveying and meteringdevice, a conveyor belt, cork screw, gravity chute, or the like.According to one example, an air source may provide a sub-stoichiometricquantity of oxygen to the primary gasifier 102 through a duct 203. Forexample, the air source may feed air or an oxygen rich gas into theprimary gasifier 102 via a gas distribution grid. According to oneexample, the gas distribution grid may distribute the air or oxygen richgas uniformly or in a preferential pattern into and over a base of theinventory provided in the primary gasifier 102. According to oneexample, steam may be injected into the primary gasifier 102 through aduct 234. Furthermore, recycle fuel gas may be injected into the primarygasifier 102 through a duct 235. According to one example, the steam andrecycle fuel gas may be regulated to control conditions within theprimary gasifier 102.

According to one example, primary gasifier fuel gas may be extractedfrom the primary gasifier 102 through a duct 204. According to oneexample, the duct 204 may carry the primary gasifier fuel gas into aprimary gasifier cyclone 236. According to one example, any particulatesremoved from the primary gasifier fuel gas may exit down a dipleg andmay be conveyed to the secondary gasifier 106 through a duct 237.According to one example, the fuel gas that exits the primary gasifiercyclone 236 is transported to the fuel gas reformer 109 through a duct238.

According to one example, primary gasifier residue solids exit theprimary gasifier 102 through a duct 239 and are transported to a charconveyor 240 before delivery to the secondary gasifier 106. According toone example, the char conveyor 240 is jacketed with cooling water fed bypipes 241, 242. According to one example, blanket nitrogen is fed intothe char conveyor 240 through a duct 243. According to one example, aportion of the injected nitrogen exits the char conveyor 240 with thecooled char ash primary gasifier residue via a duct 244. According toone example, a balance of the blanket nitrogen may be drawn into theprimary gasifier 102 through a duct 245. According to one example, thecooled char ash primary gasifier residue, along with a portion of theblanket nitrogen, may be conveyed via an auger into the secondarygasifier 106. The secondary gasifier 106 also may receive the fly ashfrom the primary gasifier cyclone 236 through a duct 237 and the fly ashfrom the secondary gasifier cyclone 247 through a duct 246 via theauger.

According to one example, the secondary gasifier 106 may receive asub-stoichiometric quantity of oxygen via a duct 207 from an air sourcehaving air or an oxygen rich gas. According to one example, thesecondary gasifier 106 may include a gas sparger that distributes theair or oxygen rich gas uniformly or in a preferential pattern into andover the solids inventory. According to one example, the secondarygasifier 106 may be a rotating kiln. According to one example, steam maybe injected into the secondary gasifier 106 through a duct 248.Furthermore, recycle fuel gas may be injected into the secondarygasifier 106 through a duct 249. According to one example, the steam andrecycle fuel gas may be regulated to control conditions within thesecondary gasifier 106. According to one example, processed fuel may befed directly into the secondary gasifier 106 through duct 290 in orderto increase an overall capacity of the multi-stage gasification system200. Furthermore, processed fuel may be fed directly into the secondarygasifier 106 through duct 290 for waste requiring high temperaturethermal treatment.

According to one example, secondary gasifier ash residue solids areremoved from the secondary gasifier 106 through a duct 250. Thesecondary gasifier ash residue solids may be and transported through anash conveyor 251 that is jacketed with cooling water or glycol fed bypipes 252, 253. Additionally, or in the alternative, the ash conveyor251 may be cooled by a countercurrent air flow generated by an airsource through a duct 254. Heated air from the ash conveyor 251 may bedirected into the secondary gasifier 106 via a duct 255. According toone example, cooled inert ash may be removed from the ash conveyor 251through a duct 256.

According to one example, the residual ash material may be anon-leachable, carbon-free, inert ash product such as a carbon freesintered mineral ash that does not require special storage or disposal.According to one example, the cooled inert ash may be a residual ashmaterial that is carbon free and may be used for aggregate orarchitectural fill. For example, the residual mineral material may beused as an aggregate material in cementitious products. Alternatively,the cooled inert ash may be safely disposed in a landfill. In this way,the residual mineral material is a value added product rather than anenvironmental liability such as ash product produced from conventionalthermal treatment plants.

According to one example, secondary gasifier fuel gas may be extractedfrom the secondary gasifier 106 through a duct 208. According to oneexample, the duct 208 may carry the secondary gasifier fuel gas into asecondary gasifier cyclone 247. According to one example, anyparticulates removed from the secondary gasifier fuel gas may exit downa dipleg and may be conveyed to the secondary gasifier 106 through aduct 246. For example, the particulates may be augered back into thesecondary gasifier 106. According to one example, the fuel gas thatexits the secondary gasifier cyclone 247 is transported to the fuel gasreformer 109 through a duct 257.

According to one example, the fuel gases that exit the primary andsecondary gasifier cyclones 236, 247 are transported to the fuel gasreformer 109 via ducts 238, 257. According to one example, an air source210 provides a sub-stoichiometric quantity of oxygen to the fuel gasreformer 109. Additionally, a blower 265 provides the recycled flue gasfrom the heat recovery system 120 to the fuel gas reformer 109 through aduct 211. The oxygen and recycled flue gas may provide the fuel gasreformer 109 with aspiration of the fuel gas streams. According to oneexample, steam injected through duct 258 may be regulated to controlconditions within the fuel gas reformer 109. For example, the steam maybe injected to control an exhaust temperature of the fuel gas reformer109. According to one example, recycled flue gas provides the steam andcarbon dioxide injected to control conditions within the fuel gasreformer 109.

According to one example, exhaust fuel gases may be extracted from thefuel gas reformer 109 through a duct 212. According to one example, theduct 212 may carry the exhaust fuel gases into the fuel gas burner 113for burning with excess air obtained from an air source via a duct 214and with recycled flue gas obtained from a duct 215. The resulting fluegases may be transported to the flue gas quench 117 via a duct 216.According to one example, recycled flue gas may be introduced into theflue gas quench 117 via a duct 218 in order to cool the resulting fluegases received from duct 216 to below a melting point of molten saltsthat are included with the entrained particulates in the resulting fluegases.

According to one example, quench fuel gases may be extracted from theflue gas quench 117 into the heat recovery steam generator (HRSG) boiler120 via a duct 219. The quench fuel gases transfer a portion of theirsensible heat to the pre-heated boiler feed water via pipe 221 thatpasses through the HRSG economizer 259. According to one example, theHRSG boiler 120 generates steam that is fluidly coupled with a steamturbine generator set 272 via pipe 222, a condensate well, pump andsteam ejector system 279 via pipe 260, and the primary and secondarygasifiers 102, 106 via pipe 261. The HRSG boiler 120 also preheats thefeed water received by the HRSG/economizer 259 through a pipe 263 to aninlet stream temperature specification. According to one example, theboiler feed water blow down may be discharged via pipe 264.

According to one example, a portion of the total flue gas that exits theHRSG boiler 120 via duct 223 may be diverted to the recycled flue gasblower 265 via duct 224. The output recycled flue gas blower 265 may bedivided into the various streams via duct 266. For example, the variousstreams may feed the fuel gas reformer 109 via the duct 211, the fuelgas burner 113 via the duct 215, the flue gas quench 117 via the duct218, the primary gasifier 102 via the duct 235, and the secondarygasifier 106 via the duct 249.

According to one example, a remaining portion of the total flue gas thatexits the HRSG boiler 120 via duct 223 may be directed to the AirPollution Control Systems #1 (“APCS #1”) 126 via duct 225. In the APCS#1 126, dry sorbent may be injected to remove acid gas, electrostaticprecipitation may be performed to remove particulates, selectivecatalytic reaction may be performed to reduce carbon monoxide, and/orselective catalytic reduction may be performed to remove NOx in order toclean the flue gases.

According to one example, the exhaust gases from the APCS #1 126 aredrafted through the HRSG economizer 259 via a duct 227. The cooled fluegas from the HRSG economizer 259 is then drafted through the AirPollution Control Systems #2 (“APCS #2”) 268 via a duct 267. Accordingto one example, the APCS #2 includes activated carbon and performs a dryacid gas treatment or sorbent injection prior to entry into a fabricfilter-bag house for final particulate removal. According to oneexample, the cooled and cleaned flue gas may be drafted into the fluegas blower and stack 270 via a duct 269. The flue gas blower and stack270 may include a blower that discharges the exhaust via a duct 271 tothe atmosphere through an exhaust stack.

According to one example, a duct 222 delivers superheated steam from theHRSG boiler 120 into the steam turbine generator set 272. Thesuperheated steam is expanded in the steam turbine generator set 272,which generates electric power that is transported by wires 273.According to one example, the expanded exhaust steam is directed to anair-cooled condenser 275 via duct 274. The expanded exhaust steam iscondensed with ambient air provided by an air source through duct 276.According to one example, the ambient air may be drafted by fans acrosscondenser tubes provided in the air-cooled condenser 275. The ambientair may exit the air-cooled condenser 275 as heated air via a duct 277.

According to one example, condensed steam is ejected from the air-cooledcondenser 275 via a pipe 278 and delivered to the condensate well, pumpand steam ejector system 279, along with ejector steam through a duct260. The condensate 280 from the condensate well, pump and steam ejectorsystem 279 is pumped into the deaerator tank 281 via pipe 280. Accordingto one example, deaeration is performed through introduction of boilerfeed water (BFW) make-up via pipe 282 and introduction of steam via duct283. According to one example, deaerated BFW is pumped from thedeaerator tank 281 through pipe 284 via a BFW Pump 285. According to oneexample, a small portion of the deaerated BFW is utilized tode-superheat the ejector and gland seal steam via a pipe 260. Theremainder of the discharge from the BFW Pump 285 is sent to the BFWpreheater section of the HRSG boiler 120 via pipe 262.

According to one example, the water treatment plant 288 supplies thesanitary water to the fuel processing facility via pipe 233, the BFWmake-up to the deaerator tank 281 via pipe 282, the effluent dischargevia pipe 287, and the water provided through pipe 286 that is used tode-superheat steam used for the primary gasifier 102, the secondarygasifier 106, and the gas reformer 109, among other components.According to one example, the water treatment plant 288 generates thewater from the leachate/wastewater received via pipe 231 from thefacility's fuel processing building 229, from the HRSG blow downreceived via pipe 264 from the HRSG boiler 120, and the make-up waterintroduced through pipe 289 to maintain a water balance at the watertreatment plant 288.

FIG. 3 illustrates an isometric representation of portions of themulti-stage gasification system illustrated in FIG. 2. According to oneexample, the multi-stage gasification system 300 includes a primarygasifier 102, a secondary gasifier 106, a reformer 109, a burner 113, aquench chamber 117, a boiler 120, and an air pollution control system126, among other components. According to one example, the multi-stagegasification system 300 is a waste-to-energy conversion system thatefficiently converts solid waste and/or biomass into steam that is usedto generate power. According to one example, the multi-stagegasification system 300 is designed to minimize NOx emissions throughstaged fuel gas combustion and flue gas recycle. FIG. 3 illustrates oneof several arrangements for these components. Some components, such asducts, pipes, dampers, baffles, and structural supports are omitted soas not to obscure the relevant features being illustrated and described.

According to one example, a fuel mix obtained from a fuel processingbuilding is transported into the primary gasifiers 102,102 by a feedersuch as an augured conveying and metering device, a conveyor belt,gravity chute, or the like. According to one example, primary gasifierfuel gas may be extracted from the primary gasifiers 102,102 throughducts 304,304. According to one example, the ducts 304 may carry theprimary gasifier fuel gas into corresponding primary gasifier cyclone336,336. According to one example, any particulates removed from theprimary gasifier fuel gas may exit down a dipleg and may be conveyed tothe secondary gasifier 106 through a duct.

According to one example, the fuel gas that exits the primary gasifiercyclones 336,336 may be transported to the fuel gas reformer 109 througha duct. According to one example, primary gasifier residue solids thatexit the primary gasifiers 102,102 through a duct may be transported toa char conveyor before delivery to the secondary gasifier 106. Thesecondary gasifier 106 also may receive the fly ash from the primarygasifier cyclones 336,336 through a duct and the fly ash from thesecondary gasifier cyclone 347 through a duct. According to one example,the secondary gasifier 106 may receive a sub-stoichiometric quantity ofoxygen via a duct from an air source having air or an oxygen rich gas.Furthermore, processed fuel may be fed directly into the secondarygasifier 106 for waste requiring high temperature thermal treatmentand/or to increase an overall capacity of the multi-stage gasificationsystem 300.

According to one example, secondary gasifier ash residue solids areremoved from the secondary gasifier 106 through a conveyor. According toone example, secondary gasifier fuel gas may be extracted from thesecondary gasifier 106 through a duct that carries the secondarygasifier fuel gas into a secondary gasifier cyclone 347. According toone example, any particulates removed from the secondary gasifier fuelgas may exit down a dipleg and may be conveyed to the secondary gasifier106 through a duct. For example, the particulates may be augered backinto the secondary gasifier 106. According to one example, the fuel gasthat exits the secondary gasifier cyclone 347 is transported to the fuelgas reformer 109 through a duct.

According to one example, the fuel gases that exit the primary andsecondary gasifier cyclones 336, 347 are transported to the fuel gasreformer 109 via ducts. According to one example, an air source providesa sub-stoichiometric quantity of oxygen to the fuel gas reformer 109.According to one example, a blower 365 provides the recycled flue gasfrom the boiler 120 to the fuel gas reformer 109 to cool gases therein.The oxygen and recycled flue gas provide the fuel gas reformer 109 withaspiration of the fuel gas streams. According to one example, steaminjected through duct may be regulated to control conditions within thefuel gas reformer 109. For example, the steam may be injected to controlan exhaust temperature of the fuel gas reformer 109.

According to one example, exhaust fuel gases may be extracted from thefuel gas reformer 109 through a duct. According to one example, theexhaust fuel gases are carried into the fuel gas burner 113 for burningwith excess air obtained from an air source and with recycled flue gasobtained from a duct 315. The resulting flue gases may be transported tothe flue gas quench 117 via a duct. According to one example, recycledflue gas may be introduced into the flue gas quench 117 via a duct 318in order to cool the resulting flue gases below a melting point ofmolten salts that are included with the entrained particulates in theresulting flue gases.

According to one example, quench fuel gases may be extracted from theflue gas quench 117 into the heat recovery steam generator (HRSG) boiler120 via a duct 319. The quench fuel gases transfer a portion of theirsensible heat to the pre-heated boiler feed water that passes throughthe HRSG economizer 259. According to one example, the HRSG boiler 120also preheats the feed water to the HRSG/economizer 259 inlet stream 263temperature specification.

According to one example, a portion of the total flue gas that exits theHRSG boiler 120 may be diverted to the recycled flue gas blower 365 viaduct 324. The output recycled flue gas blower 365 may be divided intothe various streams via duct 366. For example, the various streams mayfeed the fuel gas reformer 109 via a duct, the fuel gas burner 113 viathe duct 315, the flue gas quench 117 via the duct 318, the primarygasifier 102 via a duct, and the secondary gasifier 106 via a duct.

According to one example, a remaining portion of the total flue gas thatexits the HRSG boiler 120 may be directed to the Air Pollution ControlSystems #1 (“APCS #1”) 126 via an exhaust gas flue duct 325. In the APCS#1 126, dry sorbent may be injected to remove acid gas, electrostaticprecipitation may be performed to remove particulates, selectivecatalytic reaction may be performed to reduce carbon monoxide, and/orselective catalytic reduction may be performed to remove NOx in order toclean the flue gases. According to one example, the exhaust gas flueduct 325 may turn 180°.

According to one example, the exhaust gases from the APCS #1 126 aredrafted through the HRSG economizer 259 via a duct 327. The cooled fluegas from the HRSG economizer 259 is then drafted through the AirPollution Control Systems #2 (“APCS #2”) 268. According to one example,the APCS #2 includes activated carbon and performs a dry acid gastreatment or sorbent injection prior to entry into a fabric filter-baghouse for final particulate removal. According to one example, thecooled and cleaned flue gas may be drafted into the flue gas blower andstack 370. The flue gas blower and stack 270 may include a blower thatdischarges the exhaust to the atmosphere through an exhaust stack.

FIG. 5 is a flowchart of an example method 500 according to the presentdisclosure for thermally processing waste to produce steam and generateenergy while minimizing air pollutants in a staged thermal reactor. Themethod 500 may be implemented using the above described systems. Forexample, the method 500 may be implemented using the multi-stage or asingle-stage gasification system. In operation 502, the waste isgasified to convert the waste to a fuel gas and a substantially carbonfree, inert, granulated, sintered mineral ash. In operation 504, thefuel gas is reformed auto-thermally to minimize creation of nitrogenoxide when the fuel gas is combusted. In operation 506, the reformedfuel gas is burned to minimize creation of nitrogen oxide in a flameregion of a fuel gas burner. In operation 508, the cooled flue gas isrecirculated to control oxygen content and temperature during the wastegasification, the reforming operation, and the burning operation.According to one example, sensible heat may be extracted from the cooledflue gas and applied to generate steam.

FIG. 6 is a flowchart of an example method 600 according to the presentdisclosure for reforming fuel gas for destruction of contained ammonia.In operation 602, fuel gas is introduced into a non-catalyzed chamberthat receives ambient air and recycled flue gas containingsub-stoichiometric levels of oxygen. In operation 604, a mixture ofgases is heated in the non-catalyzed chamber to above 1800° F. for atleast 2 seconds.

According to one example, flue gas is recirculated to system componentsin order to maintain temperatures within safe operating ranges for therefractory. For example, the flue gas may be recirculated to thehigh-temperature starved-air combustor that operates as a reformer ofthe fuel gases produced in the primary and residue gasifiers. Accordingto one example, the recirculated flue gas may provide a close approachto complete combustion, while sustaining a reducing gas environment andlimiting a total energy content of the partially oxidized fuel gases.According to one example, combustion of the relatively tar free fuel gasmay be controlled by recirculating the flue gas. This minimizesformation of “thermal” NOx through limiting the localized flametemperature and oxygen content at the flame front in the excess aircombustion stage. According to one example, the recirculated flue gasprevents sintering in a shallow fluid bed gasifier. Furthermore, therecirculated flue gas enables control over sintering of the ash residuein the residue gasifier.

According to one example, the technology provides a multi-stage or asingle-stage gasification system that decouples combustion stages fromthe steam production stages. According to one example, this may beaccomplished using heat recovery steam generators. According to oneexample, staged combustion is employed to tightly control both oxygenpartial pressure and temperature at each stage to reduce NOx formation.The technology minimizes the use of costly post combustion NOx controldevices by employing a novel combination of combustion control devicesthat reduce NOx emissions through staged combustion using low excess airand flue gas recirculation. According to one example, the technologyconverts waste-to-energy with benefits of low NOx formation, low tar,low carbon ash, non-leachable ash, boiler tube protection, among otherbenefits.

The technology described herein operates auto-thermally on high moisturefuels. In other words, the technology uses only the heating value of thewaste fuel and does not require additional fuels in order to convert thewaste. According to one example, fixed carbon may be rejected from thefirst thermal reactor and may be conveyed to a secondary gasifier thatoperates at a higher temperature. The fixed carbon may be converted tofuel gas in the secondary gasifier and may be combusted to generatethermal energy. The thermal energy maybe used to create steam forindustrial applications or for generating electrical power, among otherapplications. In contrast, the fixed carbon that is rejected from thefirst thermal reactor would be lost in a conventional system.

According to one example, the technology described herein differs fromconventional technology at least through use of a second stage hightemperature starved air combustor that functions as a reformer of thefuel gases produced in the primary and secondary or residue gasifiers.According to one example, the reformer converts a majority of fuelnitrogen, which predominantly forms ammonia during the primary andresidue gasification stages, to relatively inert gaseous nitrogen, N₂.To the extent conventional municipal solid waste combustors utilizestaging of combustion in which a “starved air” stage follows an “excessair” stage, these systems are limited by a need to avoid slagging whiledestroying the fuel NOx forming precursors in the “starved air” stage.Furthermore, conventional systems control fuel NOx formation byutilizing plasma torches that reform the ammonia and other nitrogenspecies to molecular nitrogen. Several drawbacks exist with conventionalsystems, including cost and/or operating challenges associated withcatalytic reforming. For example, catalytic reforming suffers fromincreased power consumption and maintenance costs.

According to one example, an apparatus is provided that receives wasteand generates energy by producing steam from the waste. According to oneexample, the apparatus minimizing air pollutants by thermally processingthe waste to produce a carbon free residual mineral. The apparatusincludes a gasifier that receives the waste, recycled flue gas, and airto produce a fuel gas and a reformer that is fluidly coupled to thegasifier, the reformer receives the fuel gas, a first stream of recycledflue gas, and a first stream of air to auto-thermally produce a reformedfuel gas and destroy pollutants in the fuel gas at a first temperature.According to one example, the reformer is non-catalytic. The apparatusfurther includes a burner that is fluidly coupled to the reformer, theburner receives a second stream of recycled flue gas and a second streamof air to oxidize the reformed fuel gas at a second temperature thatprevents formation of nitrogen oxide, the second temperature being lowerthan the first temperature. The apparatus includes a quench chamber thatis fluidly coupled to the burner, the quench chamber receives flue gasfrom the burner that is quenched with a third stream of recycled fluegas and a boiler that is fluidly coupled to the reformer, the burner,and the quench chamber to provide the first, second, and third streamsof recycled flue gas, respectively.

According to one example, the gasifier includes one of a rotary kilnoperating with counter current flow of gases and solids, a shallowfluidized bed with fluidized bed height to a diameter ratio of less than0.1. According to another example, the gasifier includes a secondarygasifier such as a rotary kiln that generates an inert, carbonlesssintered ash. According to another example, the gasifier receivesunderfire air that is preheated by passing over the hot sintered ashthat exits the secondary gasifier in order to improve overall processthermal efficiency.

According to one example, the apparatus may include an air pollutioncontrol system that is fluidly coupled to the boiler for removal ofpollutants from the flue gas of the boiler. According to one example,the air pollution control system may be provided downstream from a pointof ammonia injection at a duct length of at least three seconds, whereinthe ammonia injection may be used to control nitrogen oxide emissions.According to one example, the apparatus may include a secondary thermaloxidative treatment system that produces a carbon-less, inert ash toachieve higher overall process thermal efficiency.

Currently in the U.S.A., 40 CFR 60 Subpart AAAA provides air emissionsstandards for municipal solid waste (MSW) combustion systems. Theseguidelines place limits on the concentrations of regulated stackemissions as well as total annual emissions of criteria pollutants.According to the US-EPA AP-42 standards document, NOx emissions formunicipal waste combustors are estimated to be 70% to 80% from thenitrogen content of the waste. Fuel NOx has been computed to correspondto be roughly 40% to 50% of the fuel nitrogen content in municipalcombustors. Referring to EPA standard AP-42 paragraph 2.1.3.5, whichnotes that 70%-80% of NOx generation in municipal waste combustors isfrom fuel nitrogen, the technology described herein enables a 70% to 80%reduction in NOx emissions. Alternatively, power generation capacity maybe increased 3.3 to 5 times while maintaining the pre-reductionemissions levels.

Examples are described above with the aid of functional building blocksthat illustrate the implementation of specified functions andrelationships thereof. The boundaries of these functional buildingblocks have been arbitrarily defined herein for the convenience of thedescription. Alternate boundaries can be defined so long as thespecified functions and relationships thereof are appropriatelyperformed. While the foregoing illustrates and describes examples ofthis technology, it is to be understood that the technology is notlimited to the constructions disclosed herein. The technology may beembodied in other specific forms without departing from its spirit.Accordingly, the appended claims are not limited by specific examplesdescribed herein.

We claim:
 1. An apparatus that receives waste and generates energy byproducing steam from the waste, the apparatus minimizing air pollutantsby thermally processing the waste to produce a carbon free residualmineral, the apparatus comprising: a gasifier that receives the wasteand air to produce a fuel gas; a reformer fluidly coupled to thegasifier, the reformer receives the fuel gas, a first stream of recycledflue gas, and a first stream of air to auto-thermally produce a reformedfuel gas and destroy pollutants in the fuel gas at a first temperature;a burner fluidly coupled to the reformer, the burner receives a secondstream of recycled flue gas and a second stream of air to oxidize thereformed fuel gas at a second temperature that prevents formation ofnitrogen oxide, the second temperature being lower than the firsttemperature; a quench chamber fluidly coupled to the burner, the quenchchamber receives flue gas from the burner that is quenched with a thirdstream of recycled flue gas; and a heat recovery system fluidly coupledto the reformer, the burner, and the quench chamber to provide thefirst, second, and third streams of recycled flue gas, respectively. 2.The apparatus according claim 1, wherein the gasifier includes one of arotary kiln or a fluidized bed.
 3. The apparatus according claim 1,wherein the gasifier includes a secondary gasifier, the secondarygasifier being a rotary kiln.
 4. The apparatus according claim 1,further comprising a cyclone that is fluidly coupled between thegasifier and the reformer, the cyclone being configured to removeparticulate matter from the fuel gas.
 5. The apparatus according claim1, wherein the heat recovery system includes a heat recovery steamgenerator that recovers heat from a flue gas received from the quenchchamber, the apparatus further comprises ducts that route a portion ofthe recycled flue gas that exits the heat recovery steam generator to atleast one of the reformer, the burner, and the quench chamber.
 6. Theapparatus according claim 3, wherein the secondary gasifier includes hotsintered ash, and the gasifier receives underfire air that is preheatedby passing over the hot sintered ash that exits the secondary gasifier.7. The apparatus according claim 1, further comprising an air pollutioncontrol system that is fluidly coupled to the boiler, the air pollutioncontrol system removes pollutants from the flue gas of the heat recoverysystem.
 8. The apparatus according claim 7, wherein the air pollutioncontrol system comprises at least one of an electrostatic precipitator,an acid gas removal device, a catalytic reduction device, or baghouse.9. The apparatus according claim 7, further comprising an economizer,wherein a portion or all of the air pollution control system is placedbetween the heat recovery system and the economizer.
 10. The apparatusaccording claim 1, wherein the gasifier is configured to produce acarbon-less, substantially inert ash and the apparatus further comprisesa secondary thermal oxidative treatment system that produces acarbon-less, inert ash.
 11. The apparatus according claim 1, wherein thewaste includes at least one of municipal solid waste, refuse derivedfuel, biomass, ancillary fuel, inorganic oxide, or inorganic carbonateand wherein the refuse derived fuel has a moisture content betweenapproximately 10% and 50% by weight.
 12. The apparatus according claim3, wherein the first, second, and third streams of recycled flue gascontrol a temperature and a fuel gas composition in at least one of thegasifier, the secondary gasifier, and the reformer.
 13. A method ofthermally processing waste to produce steam and generate energy whileminimizing air pollutants in a staged thermal reactor, the methodcomprising: gasifying the waste to convert the waste to a fuel gas and asubstantially carbon free, inert, granulated, sintered mineral ash;reforming the fuel gas auto-thermally to minimize creation of nitrogenoxide when the fuel gas is combusted; burning the reformed fuel gas tominimize creation of nitrogen oxide in a flame region of a fuel gasburner; and recirculating cooled flue gas to control oxygen content andtemperature during the reforming operation and the burning operation.14. The method according claim 13, wherein the recirculated cooled fluegas controls a temperature and a fuel gas composition during reformingof the fuel gas.
 15. The method according claim 13, wherein reformingthe fuel gas converts non-molecular nitrogen species into molecularnitrogen in an auto-thermal non-catalytic reformer unit by decompositionreactions promoted by a prevailing reducing gas atmosphere, wherein thehigher heating value content of the reformed gases is reduced tominimize forming nitrogen oxide when the fuel gas is combusted.
 16. Themethod according to claim 13, further comprising extracting sensibleheat from the cooled flue gas, the sensible heat being applied togenerate steam and directing hot exhaust gas from burning the reformedfuel gas into a heat recovery steam generator that produces processsteam or steam for generating electrical power.
 17. The method accordingto claim 13, further comprising indirectly transferring hot exhaust gasfrom burning the reformed fuel gas to a heat transfer fluid in a heatrecovery exchanger, wherein the heat transfer fluid is used to generateelectrical power in an Organic Rankine Cycle Engine and wherein wasteheat recovered from the Organic Rankine Cycle Engine is applied togenerate hot water.
 18. A method of reforming fuel gas for destructionof contained ammonia, the method comprising: introducing the fuel gasinto a non-catalyzed chamber that receives ambient air and recycled fluegas containing sub-stoichiometric levels of oxygen; and heating amixture of gases in the non-catalyzed chamber to above 1900° F. for atleast 2 seconds.
 19. The method according claim 18, wherein the recycledflue gas controls a temperature and a fuel gas composition in thenon-catalyzed chamber.
 20. The method according claim 18, whereinheating the mixture of gases in the non-catalyzed chamber is anauto-thermal process that converts non-molecular nitrogen species intomolecular nitrogen by decomposition reactions promoted by a prevailingreducing gas atmosphere, wherein the higher heating value content of thereformed gases is reduced to minimize forming nitrogen oxide when thefuel gas is combusted.